Process for the conversion of petroleum oils



April 2, 1929. G. EGLOFF 1,707,348

PROCESS FOR THE CONVERSION OF PETROLEUM OILS Original Filed Aug. 16, 1922 I 30 prises Patented Apr. 2", d

eusuv new". or cnrcaeo,

comm, or cmcaeo,

ILLINOIS, ABSIGNOB I'OB rm: OQNVEKSION Ol' PETROLEUM 0118.

Application fled Ana-rut 18, 18 88, was He. 582,284. Ienewed Zone 8,

This invention refers to improvements in a process and apparatus for the conversion of petroleum oils, and refers more particularly to a process in which relatively point oils are converted into oils havin a ow boiling point, or characteristics similar to asoline and the like. e invention refers particularly to a continuous process for treating oils under substantial premure of the pressure being controlled by valves interposed in the various lines connecting the separate stages, and a pressure relief va ve on the receiver. The si le figure is a diagrammatic side elevationiil view of the apparatus with parts in section.

Referring to the drawings, the oil to be treated isintroduced from any convenient source through the line 1 and is charged by means of a pump 2 through the line-3 regulated by the valve 4. The charging line 8 is connected near the top of a dep legmator or refluxing tower 5 so that the raw oil or incomin cool oil is introduced in the top thereof an acts as a coolin medium for the vapors which rise from t e conversion stage thro h the dephlegmator. The oil with a consi d erable condensate content which comthe hi h boiling point fractions separated from t e oil vapors, collects in the bot tom of the dephlegmator and drains down through the vapor line 6 against the travel of the oil vapors into the reactinfi or vaporizing chamber 7. In the center oft echamber7 is positioned a partition wall 8 which serves to retard the movement of the oil during vaporization, giving it ample time to eflect a relatively complete digestion and assume w an equilibrium while being maintained in a substantial body in the vaporizing chamber. In the bottom of the retort or chamber 7 are connected the headers 9 and 10 which have heating tubes 11 connected therebetween. 'The heating tubes and headers are mounted in a furnace 12 preferably heated by means of gasburner 13.

a In 0 oration, the oil is introduced as explaine and after serving as a dephlegmating so medium in the refluxing column, flows down with its condensate content into the vaporizing chamber 7 The artition wall 8 prevents the incoming oilrom mixing with the heated vaporizing oil in the other (porso tion of the chamber which is separate by hi h boiling h generated vapors,

pressures from to 350 a gravity of from 50 to 52 specification gasoline,

the partition. The oil thence flows down through the header 9 and after assin through the heating tu s 11, rises rou t e header 10 into the opposite end of t e vaporizing chamber designated as 7. In this portion of the chamber, a substantial part of the vaporization takes place, the free carbon and liquid residue being drawn ofl' thro h line 14 controlled by the valve 15. The h or 10 extends into the chamber 7 in the form of a standpi to prevent the carbon from draimng bac into the lower rtion of the header and becoming tra ped m the heating zone. The vapors rising in the oil pass out through the vapor line 6 controlled by valve 16 against the travel of the incoming oil. After rising through the dephlcgmator and being sub'e'cted to a refluxing action, the still vaporize ortion passes of! through the line 17, contro ed by the valve 18 to the water condenser coil 19 mounted in the condenser box 20, the distillate passing'from the discharge end of the condenser coil through line 2; regulated by the valve 22, to the receiver The receiver is ui ped with pressure relief valve 24, liquid rawofl valve 25, pressure gauge 26 and lipuid level gauge 27.

By treating the oi in this manner the reflux condensate may be recycled both through the vaporizing and heating zones without pr ucing any objectional cooling durin the conversion reaction. Also, the heat 0 the system may be economically used in retreating these high boiling point products which would otherwise have to be separate] treated, or returned through means whic would'subject them to substantial cooling.

By treating Mid-Continent gas oil of approximately 30 to 32 Baum gravity, to temperatures ranging from 600 to 900 F., and

nude, a substantial yield of approximate y of the oil treated may be 0 tained, the distillate having Baum of Na which requires an imtial boiling point below 130 F. and an end boiling polnt at or below 437 F.

I claim as my invention:

1. A continuous process for cracking hydrocarbon oil, consisting in introdu charging oil in intimate contact with evol i r d va rs owing through a dephlegmator, in ta in oil dephlegmated vapors from the dcph egmator for condensation and collec- TO UNIVERSAL OIL PRODUCT ILLINOIS, CORPORATION 01' SOUTH DAIOI'L pendent 9 heated toa cracking temperature, in introduc- V ing highly heated substances from the hes zoneto anindependent l in said u vaporizing zone from ghich inde-" heavy unvaporized residual oil poo ill-continuously withdrawn to be isolated lh'omthesystem and from which no oil is re turned to the heating zone and in maintainsuper-atmospheric pressure on the oil no 8 a undergoing conversion.

' 2. process for cracking hydrocarbon oils which comprises maintaining a bulk supply of oil in a supply zone, continuously )assing 35 oil from said supply zone through a eating element wherein it is raised to a cracking tam rature, introducing the heated oil from .v sai heating zone into a separating zone, in'

rernoving carbonaceous constituents from and separating zone, maintaining the oil constituents in said separating zone and the body ofoil in said supply zone in indirect heat interchange relationshi ,uniting vapors i evolved from c oil in said se aratin zone as with vapors released from the oil in sai supply zone, in subjec such vapors ina comm g ed to dep egmation in a dephlegf .y mouse mating zone, in introducing fresh charging oil for the process to said de hle tin zone toeflect the condensation o the insufliciently cracked vapors in returnin reflux condensate together with the fresh oil which has-been introduced to said dephlegmating zone to said supply zone and in so controlling the liquid leve in said supply zone that t e oil said supply zone intosaid sepuratin zone;

constituents therein cannot overflow from 3. A process for cracking hydrocar on oil which comprises maintaining a substantial of oil 111' supply zone, passing oil from sai supply zone through a heating zone wherein itis raised to a cracking temperature, delivering'uthe heated oil from said heating zone into a so arating zone wherein a bod of liquid oil co ects, maintaining the liqui oil constituents in said separating zone in indirect heat interchange relationship with the body of oil in said supply zone, maintaining the oil constituents in said separating zone and the oil body in said so pl zone in substantially the same horizonta p ane, controlling the liquid level in said supplyzone to prevent the overflow of oil from said supply zone into said separatin zone, subjecting vapors evolved from the oi in said separating zone to reflux condensation in a reflux a, condensing zone, in introducing charging oil for the process to said reflu-x condensing zone to condense the insuflicientl cracked vapors and introducing reflux con ensate se arated from the vapors and fresh charging oi which has been introduced to said reflux condensing zone to said supply zone.

7 GUSTAV EGLOFF. 

